BENZENE REDUCTION IN GASOLINE BY ALKYLATION WITH HIGHER OLEFINS

Abstract: A benzene-rich gasoline stream is alkylated with higher olefins in contact with a fluid bed of shape selective zeolite catalyst to produce a gasoline product stream reduced in benzene content wherein the high octane value alkylaromatics formed by benzene alkylation are of low carbon number, essentially C10-. Concurrently, a portion of olefins in the gasoline stream are converted to gasoline boiling range hydrocarbons and the sulfur content of the gasoline feedstream is lowered. Besides enhancing the octane value of the feedstream, the process results in a lower Reid vapor pressure and lower sulfur content.

Description: BENZENE REDUCTION IN GASOLINE BY ALKYLATION WITH HIGHER OLEFINS This invention relates to a process for the production of a more environmentally suitable gasoline by removing a substantial portion of benzene in gasoline by alkylation with C 5 + olefins wherein the alkylated aromatic product unexpectedly comprises essentially C 10 - aromatics, Reid vapor pressure (RVP) is reduced and sulfur content is lowered. In the United States, and some other countries, the record of the development of environmental regulations for the control of emissions from motor vehicles has moved from an early emphasis on end use control, as in the required application of catalytic converters to motor vehicles and standards on fleet fuel consumption, to a greater emphasis on changes in fuel composition. The first changes eliminated lead based octane enhancing additives in gasoline. More recently, compositional changes to gasoline dictated by environmental considerations include the reduction of low boiling hydrocarbon components, reduction in benzene content of gasoline and a requirement to substantially increase the oxygen content of formulated gasoline. Further regulations can be expected in the future, probably including regulations stipulating a reduction in the ASTM Distillation End Point of gasoline. The sum of the required changes to date presents an unprecedented technological challenge to the petroleum industry to meet these requirements in a timely manner with a product that maintains high octane value and is economically acceptable in the marketplace. Gasolines manufactured to contain a higher concentration of aromatics such as benzene, toluene and xylenes (BTX) can adequately meet the octane requirements of the marketplace for a high octane fuel. Aromatics, particularly benzene, are commonly produced in refinery processes such as catalytic reforming which have been a part of the conventional refinery complex for many years. However, their substitution for the environmentally unsuitable lead- based octane enhancers is complicated by environmental problems of their own. Environmental and health related studies have raised serious questions regarding the human health effects of benzene. The findings suggest that exposure to high levels of benzene should be avoided with the result that benzene concentration in gasoline to enhance octane number is limited and controlled to a relatively low value. When hydrocarbons boiling in the gasoline boiling range are reformed in the presence of a hydrogenation-dehydrogenation catalyst, a number of reactions take place which include dehydrogenation of naphthenes to form aromatics, dehydrocyclization of paraffins to form aromatics, isomerization reactions and hydrocracking reactions. The composition of the reformer effluent or reformate is shifted toward higher octane value product. Catalytic reforming primarily increases the octane of motor gasoline by aromatics formation but without increasing the yield of gasoline. Reformates can be prepared by conventional techniques by contacting any suitable material such as a naphtha charge material boiling in the range of C 5 or C 6 up to about 380°F (193*C) with hydrogen in contact with any conventional reforming catalyst. Typical reforming operating conditions include temperatures in the range of from about 800"F (427°C) to about 1000°F (538°C), preferably from about 890°F (477 β C) up to about 980°F (527 β C), liquid hourly space velocity in the range of from about 0.1 to about 10, preferably from about 0.5 to about 5; a pressure in the range of from about atmospheric up to about 700 psig (4900 kPa) and higher, preferably from about 100 (700 kPa) to about 600 psig (4200 Kpa) ; and a hydrogen-hydrocarbon ratio in the charge in the range from about 0.5 to about 20 and preferably from about 1 to about 10. The treatment of a reformate with crystalline aluminosilcate zeolites is known in the art and has included both physical treatments such as selective adsorption, as well as chemical treatments such as selective conversion thereof. In U.S. Patent 3,770,614 to Graven a process combination is described for upgrading naphtha boiling range hydrocarbons by a combination of catalytic reforming and selective conversion of paraffinic components to enhance yield of aromatic hydrocarbons by contact with crystalline aluminosilicate catalyst having particular conversion characteristics. In U.S. Patent 3,649,520 to Graven a process is described for the production of lead free gasoline by an integrated process of reforming, aromatics recovery and isomerization including C 6 hydrocarbons upgrading to higher octane product for blending. U. S. Patent 3,767,568 to Chen, discloses a process for upgrading reformates and reformer effluents by contacting them with specific zeolite catalysts so as to sorb methyl paraffins at conversion conditions and alkylate a portion of aromatic rings contained in the reformates. Recently, a process has been developed to overcome some of the foregoing challenges in the reformulation of gasoline. The process is known as the Mobil Benzene Reduction (MBR) process and is closely related to the Mobil Olefins to Gasoline (MOG) process. The MBR and MOG processes are described in U.S. patents 4,827,069 to Kushnerick, 4,950,387 and 4,992,607 to Harandi, and 4,746,762 to Avidan, all of common assignee. The MBR process is a fluid bed process which uses shape selective, metallosilicate catalyst particles, preferably ZSM-5, to convert benzene to alkylaromatics using olefins from sources such a FCC or coker fuel gas, excess LPG, light FCC naphtha or the like. Benzene is converted, and light olefin is also upgraded to gasoline concurrent with an increase in octane value. Conversion of light FCC naphtha olefins also leads to substantial reduction of gasoline olefin content and vapor pressure. The yield-octane uplift of MBR makes it one of the few gasoline reformulation processes that is actually economically beneficial in petroleum refining. The MBR process as practiced heretofore has relied upon light olefin as alkylating agent for benzene to produce alkylaromatic, principally in the C 7 -C 9 range. However, some refineries have a surplus of higher carbon number olefins, i.e., C 5 + olefins, and it would be a benefit to the refiner if these olefins could be used in processes such as MBR. However, alkylation of benzene with such higher olefins would typically be expected to produce a sharp increase in the yield of alkylaromatics of C n carbon number and above as both mono and polyalkylated aromatics. This is not a preferred mode of operation or gasoline composition. The discovery has been made that a benzene-rich gasoline stream can be alkylated with higher olefins in contact with a fluid bed of shape selective zeolite catalyst to produce a gasoline product stream reduced in benzene content wherein the high octane value alkylaromatics formed by benzene alkylation are of low carbon number, essentially C 10 -. Concurrently during the alkylation reaction, a portion of olefins in the gasoline stream are converted to gasoline boiling range hydrocarbons and the sulfur content of the gasoline feedstream is lowered. Besides enhancing the octane value of the feedstream, the process results in a lower Reid vapor pressure. A particularly surprising element of the invention is the production of substantially all C h ¬ alky1aromatics when benzene-rich gasoline is alkylated with C 5 + olefins according to the process of the invention. Ordinarily, alkylation of benzene with C 5 + olefins would be expected to produce a large quantity of C n + alkylaromatics by mono or poly alkylation with olefins. The novel chemistry of the instant process unexpectedly avoids the formation of such higher alkylaromatics leading to the formation of a high octane value gasoline product predominantly in the C 5 -C 9 range. The process comprises contacting the benzene- rich stream and the C 5 + olefin stream with solid, shape selective aluminosilicate catalyst particles in a fluidized catalyst bed under benzene alkylation conditions whereby an effluent stream is produced comprising gasoline having a reduced benzene content and containing aromatics comprising substantially C 10 - alkylated aromatics. The present invention comprises an improvement to the Mobil Benzene Reduction process (MBR) generally described above. The invention provides a process for lowering the benzene content, olefin content, Reid vapor pressure and sulfur content of any benzene rich C 5 + gasoline boiling range hydrocar¬ bon feedstream while enhancing octane value. While these achievements are basic endowments of the MBR process when alkylation of benzene is carried out with light olefins, the present invention embodies the discovery that higher olefins, i.e., C 5 +, can be used as alkylating agents in the MBR process without substantially increasing the production of higher, i.e., C 10 +, alkylaromatics. In a preferred embodiment the invention provides a process integrated into the reformer section of a refinery for the manufacture of high octane gasoline. The invention can improve the economics of meeting the benzene specification of the gasoline pool, preferably reducing the pool benzene content below 1% or 0.8 %. One embodiment of the process of this invention resides in the conversion of a portion of a reformate or reformer effluent, or any benzene rich C 5 + gasoline feedstream, following fractionation in a fractionation system. Portions subjected to conver¬ sion in the process are the C 6 fraction; also, the C 6 fraction plus at least a portion of the C 9 + or C 10 + fraction of the reformate containing aromatic and non-aromatic compounds. The conversion is carried out at conversion conditions with or without added hydrogen over a shape selective metallosilicate cata¬ lyst, preferably aluminosilicate. Reformates or reformer effluents which are composed substantially of paraffinic and aromatic constituents can be prepared according to conventional techniques by contacting any suitable material such as naphtha charge material or heavy straight run gasoline boiling in the range of C 5 and preferably in the range of C 6 up to about 400°F (204 °C) and higher with hydrogen at least initially in contact with any reforming catalyst. This is a conventional reforming operation which involves a net production of hydrogen and is well known to those skilled in the art as described in Chapter 6 of Petroleum Refining by James H. Gray and Glenn E. Handwerk as Published by Marcel Dekker, Inc. (1984) . Reforming catalysts in general contain platinum supported on an alumina or silica-aluminum base. Preferably, rhenium is combined with platinum to form a more stable catalyst which permits operation at lower pressures. It is considered that platinum serves as a catalytic site for hydrogenation and dehydrogenation reactions and chlorinated alumina provides an acid site for isomerization, cyclization, and hydrocracking reactions. Some impurities in the feed such as hydrogen sulfide, ammonia and organic nitrogen and sulfur compounds will deactivate the catalyst. Accordingly, feed pretreating in the form of hydrotreating is usually employed to remove these materials. Typically feedstock and reforming products or reformate have the following analysis: TABLE 1 COMPONENT (vol %. FEED PRODUCT Paraffins 45-55 30-50 Olefins 0-2 0 Naphthenes 30-40 5-10 Aromatics 5-10 45-60 Reforming operating conditions include temperatures in the range of from about 800°F (427°C) to about 1000°F (538 β C), preferably from about 890 β F (477 β C) up to about 980 β F (527 β C) , liquid hourly space velocity in the range of from about 0.1 to about 10, preferably from about 0.5 to about 5; a pressure in the range of from about atmospheric up to about 700 psig (4900 Kpa) and higher, preferably from about 100 (700 kPa) to about 600 psig (4200 Kpa) ; and a hydrogen-hydrocarbon ratio in the charge in the range from about 0.5 to about 20 and preferably from about 1 to about 10. One aspect of the present invention is the incorporation of a process step comprising the fractionation of the reformate or reformer effluent, or C 5 + hydrocarbon feedstream. The fractionation step permits separation of the reformer effluent into several streams or fractions. These streams include a C 6 hydrocarbon fraction rich in benzene; also a fraction consisting of C 6 + and a portion of C 9 + aromatic rich hydrocarbons. These latter streams contain components of reformate that compromise the environmental acceptability of that product. It has been discovered in the present invention that all or a portion of these streams can be coprocessed by the MBR process in a fluid bed conversion zone containing shape selective aluminosilicate catalyst particles to upgrade these components to environmentally acceptable and high octane value gasoline constituents. As noted earlier, any benzene rich C 5 + gasoline boiling range hydrocarbon feedstream can be used in the MBR process, conventionally with a light olefins feedstream as alkylating agent. However, reformate is preferred. Benzene alkylation processes to reduce gasoline benzene content use light olefinic gas feedstocks containing ethene, propylene or butenes as the alkylating agent. Refinery olefinic streams typically include FCC offgas, fuel gas, and LPG. The reaction takes place over appropriate catalysts to produce alkyl aromatic hydrocarbons and improve gasoline octane and yield. C 5 + olefins, it has been found, are also effective alkylating agents when used in conjunction with shape selective zeolite such as ZSM-5 catalysts in the Mobil Benzene Reduction (MBR) process. The alkylated aromatic product remain essentially as C 10 - aromatics. A number of sources of cracked gasoline streams in the refinery can be used as alkylating agent, including fluid catalytic cracking (FCC) gasoline or Thermafor catalytic cracking (TCC) gasoline, coker gasoline, and pyrolysis gasoline. Preferably, a light naphtha stream is used to maximize olefin content of the stream as olefins tend to concentrate in the C 3 -C 7 hydrocarbon range. Use of cracked gasoline feeds (i.e., C 5 + olefins) in other benzene alkylation processes will lead to formation of C n + aromatics. Also, other processes are more susceptible to catalyst poisoning which would be accelerated in the presence of naphtha feeds. While not wanting to be bound by a theory of operation, it appears that in the present invention when the benzene rich stream is coprocessed with C 5 + olefins over shape selective zeolite catalyst particles several reactions occur that lead to a substantial reduction in the benzene content of the product of the process and, simultaneously, a reduction in the Reid vapor pressure and sulfur content. These reactions, it is believed, include cracking, alkylation, and transalkylation. The C 9 + fraction containing aromatic and non-aromatic compounds, such as dialkylated aromatics, can enter into transalkylation reactions with benzene under the conditions of the process leading to the formation of C 7 -C 8 alkylated aromatics from benzene. Also, cracking paraffins, particularly higher molecular weight normal and slightly branched paraffins, results in the production of compounds that are effective in alkylating benzene and further producing alkylated aromatics under the conditions of the conversion process. Conversion of a benzene rich gasoline feedstream used in the present invention in contact with metallosilicate catalyst particles is generally carried out at a temperature between 500 β F (260 β C) and about 1000 β F (538 β C) preferably between 550-900 β F (288-482 β C) and most preferably between 700-850°F (371-454°C). The pressure is generally between about 50 (350 Kpa) and 3000 psig (21000 kPa) , preferably between 50-400 psig (350-2860 kPa) . The liquid hourly space velocity, i.e., the liquid volume of hydrocarbon per hour per volume of catalyst is between 0.1 and 250, preferably between 1 and 100. A most preferable weight hourly space velocity based on total feed is between 0.5 and 3 WHSV. If hydrogen is charged, the molar ratio of hydrogen to hydrocarbon charged can be as high as 10 but it is preferably zero. Any type of catalytic reactor can be used in the process of the invention including fluid bed, fixed bed, riser reactor, moving bed, and the like. However, fluid bed catalytic reactor is preferred. The preferred catalysts are the intermediate pore size zeolites, of which ZSM-5 is the most favored. This zeolite is usually synthesized with Bronsted acid active sites by incorporating a tetrahedrally coordinated metal, such as Al, Ga, or Fe, within the zeolitic framework. The ZSM-5 crystalline structure is readily recognized by its X- ray diffraction pattern, which is described in U.S. Patent No. 3,702,866 (Argauer, et al.), incorporated by reference. The medium pore zeolites are favored for acid catalysis; however, the advantages of these zeolite materials may be utilized by employing highly siliceous materials or crystalline metallosilicate having one or more tetrahedral species having varying degrees of acidity. The preferred catalysts for use in the conversion step of the present invention include the medium pore crystalline aluminosilicate zeolites having a silica to alumina ratio of at least 12, and constraint index of about 1 to 12. Representative of the zeolites of this type are ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, MCM-22, and ZSM-48. Other acidic materials may also prove useful. Representative of the larger pore zeolites (constraint index no greater than 2) , which are useful as catalysts in the process of this invention, are zeolite Beta, TEA mordenite, zeolite Y, especially USY and ZSM-12. Zeolite Beta is described in U.S. Reissue Patent No. 28,341 (of original U.S. Patent No. 3,308,069), to which reference is made for details of this catalyst. Zeolite ZSM-12 is described in U.S.Patent No.3,832,449, to which reference is made for the details of this catalyst. The method by which Constraint Index is determined is described fully in U.S. Patent No. 4,016,218, to which reference is made for details of the method. The preferred catalyst for use in the present invention is acidic ZSM-5 having an equilibrium alpha value less than 100, preferably less than 50. Alpha value, or alpha number, is a measure of zeolite acidic functionality and is more fully described together with details of its measurement in U.S. Patent No. 4,016,218, J. Catalysis. 6 , pp. 278-287 (1966) and J. Catalysis. 61. pp. 390-396 (1980) . A series of bench-scale pilot unit experiments (Examples 1-5 as described herein) were conducted which showed effective benzene reduction using heavier olefins as the alkylating agent. Two different cracked stocks were evaluated: a) light (215 β F) FCC gasoline and b) full range pyrolysis gasoline. Feedstock properties for these are given in Tables 3 and 4, respectively. These cracked gasolines were blended with benzene-rich reformate cuts in various proportions and charged to a fluid bed reactor containing acidic ZSM-5 catalyst. Operating conditions were as follows: TABLE 2 Example 1 2 3 4 5 Olefin Source Lt FCC Lt FCC pygas pygas pygas gasoline gasoline Vol % Olefin Source in blend 50 75 30 30 14 Temp, β F 800 800 750 800 800 Press. , psig 75 75 180 150 190 WHSV on feed. hr" 1 1.5 1.0 1.0 1.0 1. Material balances on Examples 1-5 were taken at 3 and 8 hours-on-stream. These detailed material balance data are shown in Tables 5 - 9. Tables 5 - 9 show that benzene conversions for Examples 1-5 between 25% and 42% were obtained while producing only a very small amount of C + alkyl aromatics, i.e., between 1.5 wt % and 7.5 wt %. A number of clean fuel benefits other than benzene reduction were also achieved. Reductions of at least 60 weight percent, or between 72% and 81%, for C 5 + olefins and between 0.5 and 1 psi for RVP were obtained. The ratio of C 9 to C 10 aromatics is at least 2.5:1. Significant sulfur conversion was also found, i.e., greater than 60 wt %. The detailed sulfur GC analysis on the feed and liquid product for MB-1 (three hours on stream) of Example 2 (Table 10) shows over 70% conversion of both ring (thiophenic) and mercaptan sulfur species. An octane boost is also obtained. The magnitude of the uplift depends on the feedstock composition and reaction severity. The use of C 5 + olefin feed as the sole alkylating agent in benzene reduction processes produces novel results as shown in Tables 5-10. The prior art specifies the use of light olefinic gas feeds (C 2 -C 4 olefins). Over ZSM-5, heavy olefins are alkylated to form C 7 -C 10 aromatics rather than heavier C n + aromatics. A number of unexpected clean fuel benefits including sulfur reduction are also obtained. These findings show that MBR effectively converts benzene using heavy olefins as the alkylating agent and provides added flexibility to the process. This can be especially attractive to refiners with limited light olefin availability. TABLE 3 Feedstock Properties- Light FCC Naphtha (215- "P) Composition . wt% Hydrogen 0. 0 Methane 0. 0 Ethane 0.0 Ethene 0. 0 Propane 0. 0 Propene 0. 0 N-Butane 0.9 Isobutane 0.4 Butenes 3.5 Total C 5 + 95.2 C 5 -C 9 Isoparaffins 30.1 C 3 -C 9 N-Paraffins 7.5 C 5 -C 9 Olefins 44.4 C 5 -C 9 Naphthenes 7. 3 C 6 -C 9 Aromatics 5.8 C 10 + & unknowns 0. 1 Benzene 2.3 Toluene 3.4 Total Sulfur, ppmw 242 Mercaptan Sulfur, ppmw 3 Nitrogen, ppmw 7 C j + Properties R + O/M + O 90.4/79.2 Molecular Weight 82.2 Density @ 60*F, g/ml 0.68 Reid Vapor Pressure, psia 9.9 TABLE 4 Feedstock Properties- Pyrolysis Gasoline Composition, wt % Butenes 1.1 Pentenes 9.9 Pentadienes 2.3 Other C 5 0.9 Benzene 13.1 C 6 Olefins 16. 6 Other C 6 0. ,2 Toluene 6. ,9 C 7 Olefins 8. ,6 Other C 7 0. ,6 C 8 aromatics 3. ,2 C 8 Olefins 4. ,8 Other C 8 0. ,9 C 9 Olefins 6. ,2 Other C 9 4. .3 Other C 10 + 20. .5 Total C 9 - Olefins, wt% 49. .5 Total Sulfur, wt% 0. .051 Mercaptan Sulfur, ppmw 129 Nitrogen, ppmw 29 Bromine Number 101. .1 Dienes, mmol/g 1. .3 R + O 94. .4 M + O 77, .5 RVP, psia 7, .3 TABLE 5 Example l: Material Balance Data Feed: 50/50 v/v FCC Lt. Naphtha/Reformate Cut Blend Material Balance Number Feed 1 2 Hours on Stream - 2 8 Reactor Pressure, psig 75 75 Avg. Reactor Temperature, °F - 800 799 Total HC Feed WHSV, hr _1 1.5 1.5 Benzene/C.-C, Olβf ins ,mol/mol 0.94 0.94 0.94 Benzene/C.-C, Olefins, wt/wt 0.93 0.93 0.93 C--C, Olefin Conversion, % 63.7 50.1 C 5 -C, Olefin Conversion, % 74.6 70.1 Benzene Conversion, % 32.3 29.5 Composition , wt % of hydrocarbon Hydrogen 0.00 0.01 0.03 Methane 0.00 0.02 0.06 Ethane 0.00 0.08 0.16 Ethene 0.00 0.09 0.33 Propane 0.00 2.77 2.93 Propene 0.00 0.77 1.60 N-Butane 0.24 2.45 2.07 I βobut ane 0.09 3.33 2.69 Butenes 1.00 1.88 2.92 Total C s + 96.67 88.60 87.21 C.-C, Isoparaffins 33.81 34.09 33.26 C 9 -C 9 N-Paraffins 13.10 10.50 10.76 C,-C, Olefins 21.77 5.53 6.51 C.-C, Naphthenes 5.61 5.22 5.37 C 6 -C, Aromatics 24.32 27.00 27.43 C 10+ & Unknowns 0.05 6.25 3.87 Benzene 21. 18 14.33 14.94 Toluene 3.09 4.05 3.88 Ethylbenzene 0.02 2.32 2.06 Xylenes 0.04 1.02 1.30 C, Aromatics 0.00 5.28 5.25 C 10 Aromatics 0.01 1.88 1.54 C 10 P+O+N 0.02 0.71 0.77 C..+ & Unknowns 0.03 3.66 1.56 C.+ Properties R+O/M+O 86.5/79. .0 89.0/82. .8 88.9/82.1 Molecular Weight 83.0 89.4 88.2 Density β 60°F, g/ml 0.71 0.73 0.73 Reid Vapor Pressure, psia 7 7..44 6.4 6.5 Sulfur, ppmw 25 60* 78* (a)- total liquid product TABLE 6 Example 2 : Material Balance Data Feed : 75/25 v/v FCC Liσht Naphtha . 215- 0 F . / Reformate Cut Blend Material Balance Number Feed 1 2 Hours on Stream 3 9 Reactor Pressure, psig 75 75 Avg. Reactor Temperature, °F 801 801 Total HC Feed WHSV, hr _1 1.0 1.0 Benzene/C.-C, Olefins, mol/mol 0.42 0.42 0.42 Benzene/C.-C, Olefins, wt/wt 0.41 0.41 0.41 Cj-C, Olefin Conversion, % 75.5 61.6 C 3 -C, Olefin Conversion, % 86.4 76.8 Benzene Conversion, % 43.5 42.6 Composition, wt % of hydrocarbon Hydrogen 0.00 0.05 0.04 Methane 0.00 0.14 0.10 Ethane 0.00 0.36 0.25 Ethene 0.00 0.32 0.43 Propane 0.00 6.16 4.64 Propene 0.00 1.24 1.76 N-Butane 0.35 3.86 3.14 Isobutane 0.13 5.35 4.25 Butenes 1.46 2.22 3.14 Total C 5 + 98.05 80.29 82.26 C,-C, Isoparaffins 32.28 31.41 31.72 C 5 -C, N-Paraffins 10.43 7.95 8.59 C 5 -C, Olefins 31.48 4.28 7.31 C--C, Naphthenes 6.64 5.57 6.07 Cj-C, Aromatics 17.12 25.26 22.90 C 10+ & Unknowns 0.10 5.81 5.68 Benzene 13.66 7.72 7.84 Toluene 3.40 5.48 5.08 Ethylbenzβne 0.03 2.67 2.26 Xylenes 0.03 3.98 2.56 C, Aromatics 0.00 5.41 5.16 C 10 Aromatics 0.00 1.55 1.33 C 10 P+O+N 0.04 0.30 0.29 C--+ & Unknowns 0.06 3.96 4.06 C.+ Properties R+O/M+O 87.5/79.4 90.3/82.8 90.1/82.4 Molecular Weight 82.9 90.3 90.1 Density . 60°F, g/ml 0.70 0.73 0.73 Reid Vapor Pressure, psia 8.3 7.0 7.1 Sulfur, ppmw 170 72* 97* (a) - total liquid product TABLE 7 Example 3 : Material Balance Data Feed : 30/70 v/v Pyrolvsis Gasoline/ Reformate Cut Blend Material Balance Number Feed 1 Hours on Stream 3 Reactor Pressure, psig 180 Avg. Reactor Temperature, β F 751 Total HC Feed WHSV, hr" 1 1.0 Benzene/C.-C, Olefins , mol/mol 3.43 Benzene/C.-C, Olefins, wt/wt 3.25 C.-C, Olefin Conversion, % 73.6 C--C, Olefin Conversion, % 81.1 Benzene Conversion, % 33.8 Composition, wt % of hydrocarbon Hydrogen 0.00 0.00 Methane 0.00 0.02 Ethane 0.00 0.09 Ethene 0.00 0.03 Propane 0.00 3.68 Propene 0.00 0.28 N-Butane 0.00 2.65 Isobutane 0.00 3.05 Butenes 0.33 0.71 Total C s + 99.67 89.48 C 3 -C, Isoparaffins 16.42 15.51 C 9 -C, N-Paraffins 15.30 9.74 C.-C, Olefins 12.42 2.35 C--C, Naphthenes 4.28 2.71 C β -C, Aromatics 46.29 47.98 C 10+ & Unknowns 4.96 11.19 Benzene 41.42 27.44 Toluene 3.08 4.39 Ethylbenzene 0.26 3.81 Xylenes 0.64 1.71 C, Aromatics 0.89 10.64 C- o Aromatics 0.72 3.40 C lβ P+O+N 0.54 0.44 C..+ & Unknowns 3.70 7.35 C.+ Properties R+O/M+O 88.3/77.3 93.9/84.3 Molecular Weight 85.7 93.1 Density β 60°F, g/ml 0.77 0.79 Reid Vapor Pressure, psia 4.9 4.0 TABLE 8 Example 4 : Material Balance Data Feed : 30/70 v/v Pvrolvsis Gasoline/ Reformate Cut Blend Material Balance Number Feed 1 2 Hours on Stream _ 3 8 Reactor Pressure, psig - 150 150 Avg. Reactor Temperature, °F - 800 800 Total HC Feed WHSV, hr' 1 - 1.0 1.0 Benzene/C.-C, Olefins , mol/mol 3.43 3.43 3.43 Benzene/C--C, Olefins , wt/wt 3.25 3.25 3.25 C.-C, Olefin Conversion, % - 65.0 56.1 C j -C, Olefin Conversion, % — 77.1 74.6 Benzene Conversion, % - 29.6 24.7 Composition , wt % of hydrocarbon Hydrogen 0.00 0.07 0.05 Methane 0.00 0.46 0.37 Ethane 0.00 0.87 0.87 Ethene 0.00 0.11 0.18 Propane 0.00 7.09 5.29 Propene 0.00 0.47 0.82 N-Butane 0.00 2.47 1.70 Isobutane 0.00 2.61 1.67 Butenes 1.33 1.04 1.45 Total C 9 + 99.67 84.81 87.61 C 9 -C, Iβoparaffins 16.42 12.31 13.97 C 9 -C, N-Paraffins 15.30 8.13 9.54 C 9 -C, Olefins 12.42 2.84 3.15 C 9 -C, Naphthenes 4 .28 2.09 2.46 C 6 -C, Aromatics 46.29 49.85 50.57 C 10+ & Unknowns 4.96 9.59 7.91 Benzene 41.42 29.17 31.19 Toluene 3.08 6.58 6.48 Ethylbenzene 0.26 5.71 5.29 Xylenes 0.64 2.12 1.99 C, Aromatics 0.89 6.27 5.62 C 10 Aromatics 0.72 2.71 2.09 C 10 P+O+N 0.54 0.26 0.22 C..+ & Unknowns 3.70 6.62 5.60 C.+ Properties R+O/M+O 88. .3/77.3 96. , 2/86.0 94. .7/84.7 Molecular Weight 85 , .7 91. .8 90. .6 Density β 60°F, g/ml 0. .77 0. .80 0 , .79 Reid Vapor Pressure, psia 4.9 3.9 4.0 Example 5 : Material Balance Data Feed : 14 /86 v/v Pvrolvsis Gasoline/ Reformate Cut Blend Material Balance Number Feed 1 2 Hours on Stream - 3 8 Reactor Pressure, psig - 190 190 Avg . Reactor Temperature, °F - 800 799 Total HC Feed WHSV, hr -1 - 1.0 1.0 Benzene/C.-C, Olefins , mol/mol 2.74 2.74 2.74 Benzene/C.-C, Olefins , wt/wt 2.59 2.59 2.59 C.-C, Olefin Conversion, % - 57.5 49.8 C j -C, Olefin Conversion, % - 77.9 76.0 Benzene Conversion, % - 45.8 42.0 Composition, wt % of hydrocarbon Hydrogen 0.00 0.15 0.03 Methane 0.00 0.44 0.42 Ethane 0.00 1.17 1.16 Ethene 0.00 0.20 0.26 Propane 0.00 10.57 9.57 Propene 0.00 0.57 0.81 N-Butane 0.00 3.99 3.76 Isobutane 0.00 3.92 3.49 Butenes 0.01 1.08 1.31 Total C 9 + 99.99 77.90 79.19 C 3 -C, Isoparaffins 33.40 23.24 25.10 C 9 -C, N-Paraffins 20.92 7.01 8.36 C--C, Olefins 9.05 2.00 2.17 C 9 -C, Naphthenes 5.46 1.91 2.11 C--C, Aromatics 27.93 35.25 34.49 C 10t & Unknowns 3.25 8.49 6.96 Benzene 23.45 12.71 13.61 Toluene 3.10 6.83 6.24 Ethylbenzene 0.20 5.81 5.99 Xylenes 0.49 4.15 3.47 C, Aromatics 0.68 5.75 5.18 C 10 Aromatics 0.56 2.34 1.92 C 10 P+O+N 0.33 0.06 0.05 C x .+ & Unknowns 2.36 6.09 4.99 C.+ Properties R+O/M+O 80. .5/74.6 95. .6/85.5 93. .3/85.1 Molecular Weight 88. .2 95 , .7 94. .3 Density β 60 β F, g/ml 0. .73 0. .77 0. .76 Reid Vapor Pressure, 4. .8 4 . . 1 4 . .2 psia Sulfur , ppmw 91 N/A 38* (a) - total liquid product TABLE 10 Example 2 - Detailed sulfur GC Results (MB-l) Feed: 75/25 v/v FCC Liσht Naphtha .215-°./ Reformate Cut Blend Feed TLP Wt % of Feed 100 84 Composition, ppm Total S 187 75 Thiophene (T) 77 15 C 2 -T 3 9 C 3 +T 0 14 Total Thiophenes 179 59 Benzothiophene (BTH) <1 1 C α -BTH 1 3 C 2 +BTH 0 4 Total BTH 1 8 Total H 2 S + Mercaptans 7 7 Dissolved H 2 S 0 5 Cj-C 3 Mercaptan 0 2 Net Conversion. wt% a Total S 67 Thiophene 84 Cj-Thiophene 82 Overall Thiophene 72 (a) Assumed negligible C 5 + range sulfur in gas product.

Claims: CLAIMS ; 1. A process for alkylating a benzene-rich gasoline boiling range hydrocarbon feedstream with a hydrocarbon stream comprising C 5 + olefins to produce product gasoline having a reduced benzene content and containing aromatics comprising substantially C 10 - alkylated aromatics, said process comprising: contacting said benzene-rich stream and said C 5 + olefin stream with solid, shape selective aluminosilicate catalyst particles in a catalyst bed under benzene alkylation condi¬ tions whereby an effluent stream is produced comprising said gasoline having a reduced benzene content and containing aromatics comprising substantially C 10 - alkylated aromatics. 2. The process of claim 1 wherein said catalyst comprises acidic ZSM-5. 3. The process of claim 1 wherein said benzene alkylation conditions comprise temperature between 500 β F and 1000"F, pressure between about 50 (350 kPa) and 3000 psig (21000 kPa) , and liquid hourly space velocity between 0.1 and about 250. 4. The process of claim 1 wherein said catalyst bed comprises a fluid bed. 5. The process of claim 3 wherein said benzene alkylation conditions comprise temperature 700- 850 β F (371-454°C), pressure between 50-400 psig (350-2860 kPa) , and liquid hourly space velocity between about 1 and 100. 6. The process of claim 1 wherein said hydrocarbon stream comprising C 5 + olefins comprises cracked gasoline. 7. The process of claim 6 wherein said cracked gasoline is selected from the group consisting of FCC gasoline, TCC gasoline, coker gasoline and pyrolysis gasoline. 8. The process of claim 1 wherein said product gasoline also has a lower Reid vapor pressure. 9. The process of claim 1 wherein said product gasoline has a lower sulfur content relative to said gasoline feedstream. 10. The process of claim 1 wherein said benzene content is lowered by at least 25 weight percent relative to said hydrocarbon feedstream. 11. A process for reduction of the benzene and olefin content of C 5 + FCC gasoline comprising: contacting a FCC gasoline feedstream with solid, shape selective aluminosilicate catalyst particles in a catalyst bed under benzene alkylation conditions whereby an effluent stream is produced comprising said gasoline having a reduced benzene and olefin content and containing aromatics comprising substantially C 10 - alkylated aromatics. 12. The process of claim 11 wherein at least a 25 weight percent reduction in benzene content and at least a 60 weight percent reduction in C 5+ olefin content is achieved. 13. The process of claim 11 wherein said catalyst comprises ZSM-5. 14. The process of claim 11 wherein said benzene alkylation conditions comprise temperature 700- 850 β F (371-454'C), pressure between 50-400 psig (350-2860 kPa) , and liquid hourly space velocity between about 1 and 100. 15. The process of claim 11 wherein said effluent stream has a lower Reid vapor pressure. 16. The process of claim 11 wherein said effluent stream has a lower sulfur content relative to said gasoline feedstream. 17. The process of claim 11 wherein said catalyst bed comprises a fluid bed.

Inventors: CHIN ARTHUR ACHHING, COLLINS NICK ALLEN, HARANDI MOHSEN NADIMI, THOMSON ROBERT THOMAS, WARE ROBERT ADAMS, CHIN, ARTHUR, ACHHING, COLLINS, NICK, ALLEN, HARANDI, MOHSEN, NADIMI, THOMSON, ROBERT, THOMAS, WARE, ROBERT, ADAMS
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1994
Main classification: C07C2
IPC codes: B01J29, C07B61, C07C2, C07C7, C07C15, C10G29, C10G35